US4163652A - Refrigerative fractionation of cracking-gases in ethylene production plants - Google Patents

Refrigerative fractionation of cracking-gases in ethylene production plants Download PDF

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US4163652A
US4163652A US05/781,064 US78106477A US4163652A US 4163652 A US4163652 A US 4163652A US 78106477 A US78106477 A US 78106477A US 4163652 A US4163652 A US 4163652A
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ethane
sub
fraction
liquid
demethanizing
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Luigi Gazzi
Oronzo Sguera
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SnamProgetti SpA
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/09—Purification; Separation; Use of additives by fractional condensation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/002—Cooling of cracked gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/906—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by heat driven absorption chillers
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • This invention relates to a method for the refrigerative fractionation of cracking-gases in an ethylene production plant.
  • the ethane cycle thus encompasses a temperature range from minus 88° C. to +25° C., which is narrower than that which is usually supplied by the two propylene and ethylene cascade cycles which cover a range of from minus 100° C. to +40° C.
  • cooling waters at a low temperature are available. This is the case, for example, with the seawater off the coasts of Northern Europe or off the coasts of the southernmost portion of South America, or with underground waters in the temperate regions, whenever used in continuous-flow cooling systems rather than for topping-up cooling towers.
  • such a power source is constituted by the flue gases of the cracking ovens, such gases being discharged in the atmosphere at a temperature in the range between +180° C. and +250° C.
  • FIG. 1 is a diagram of fractionation apparatus adapted for use in the practice of our invention
  • FIG. 2 is a diagram of the ethane refrigeration cycle
  • FIG. 3 is a diagram showing the connection of the refrigeration cycle illustrated in FIG. 2 with the fractionation apparatus illustrated in FIG. 1;
  • FIG. 4 is a diagram of a modification of the apparatus illustrated in FIG. 1;
  • FIG. 5 is a diagram of a further modification of the apparatus illustrated in FIG. 1;
  • FIG. 6 is a diagram of a further modification of the apparatus illustrated in FIG. 1.
  • the raw material for the production of ethylene such as ethane, but any other raw material can be considered, is cracked in the thermal decomposition ovens.
  • the effluent from the ovens is quenched, cooled and compressed to the usual pressure, such as 35 abs. atmospheres.
  • the effluent from the ovens that is the raw gas
  • the acidic gaseous components Upon compression, it is stripped of acetylene and dehydrated.
  • the gas, introduced through the piping 1, is cooled to minus 30° C. in the ethane refrigerator 2 (the conventional frigorie recovery stages, the frigories being those of the processing streams, have been omitted for the sake of simplicity in the area which is involved in the refrigeration of the ethane cycle), a liquid being produced which is separated at 3 and is fed, via the piping 4, to the demethanizing unit 7.
  • the gas emerging from the top of the separator 3, via the piping 6, is cooled down to minus 59° C. in the ethane refrigeration unit 5 and then fed to the demethanizing unit 7.
  • the condenser 9 of the demethanizing unit 7 is cooled with refrigerating ethane down to minus 82° C.
  • the head product emerging from the storage tank 8 contains hydrogen, methane and considerable amounts of ethylene and ethane: it is cooled in the frigorie-recovering unit 11 and then partially liquefied and sent through the piping 10 into the separator 12.
  • the gas is sent through the piping 13 to the first stage of the turbine, 14, wherein it is caused to expand, while the liquid, through the piping 15, is caused to expand in the valve 16.
  • the gas and the liquid after their relative expansions are sent to the separator 17.
  • the expansions are repeated (for a total of three times in the example shown) until reaching the final pressure in the separator 27, that which corresponds to a saturation temperature of minus 146° C. approximately.
  • the gas which contains hydrogen and methane, is sent through the main 28, to a number of frigorie-recovering units 11 (only the first has been shown) and is then heated up to the ambient temperature.
  • the liquid by means of the pump 29 and through the piping 30, is also preheated in the frigorie-recovery unit 11 and then fed into the demethanizing unit 7 as a top feeding stream.
  • the bottom product of the demethanizing unit 7, the latter being equipped with a reboiler 35, is fed through the piping 31, to the deethanizing unit 33 after having been expanded in the valve 32.
  • the deethanizing unit 33 is a quite conventional column which is equipped with the condenser 36, the reflux storage tank 37, the reflux pump 38, the reboiler 39. From the top of the column ethylene plus ethane are obtained and from its bottom, the C3 and heavier components are obtained, to be sent either to burnout or to a subsequent fractionation stage.
  • the distillate of the deethanizing unit 33 is sent via the piping 40 to the ethylene-ethane splitter 42, after having been expanded in the valve 41.
  • the splitter column 42 can be of conventional make, equipped with a condenser which is refrigerated with boiling ethane at minus 41° C., and having also a reboiler heated with ethane which is condensed at about 0° C.
  • the splitter column 42 can be integrated with the ethane refrigeration cycle, dispensing with the reboiler and taking the ethane vapors from the refrigeration cycle under a pressure of about 17.8 abs. atmospheres which corresponds to a saturation temperature of minus 12° C.
  • the ethane refrigeration cycle which integrates the installation now described, is shown in FIG. 2. It is composed by four compression stages which correspond to four temperature levels, namely:
  • the selection of the number of the stages is a merely economic question. As a rule, it can be stated that the number of the stages can be varied from three to six.
  • the refrigeration cycle is quite conventional, with the exception of the interconnection with the splitter, this detail being better described in FIG. 3.
  • liquid ethane at minus 41° C. is drawn from the refrigeration cycle and exactly from the bottom of the separator 77, and vaporized in the condenser 43 of the splitter, thus producing the reflux stream which is required for the operation of the splitter as such.
  • the thus produced vapors are recycled to the refrigeration cycle via the piping 49, and precisely to the separator 78 and then to the compressor 92.
  • ethane vapors are compressed in the third stage of the refrigeration compressor 92, together with other vapors of the cycle. A fraction of this stream is drawn and is saturated in the separator 77 and then sent, via the piping 47, to the splitter 42, such vapors having in this case the function of boil-up vapors.
  • the balance of the stream from compressor 92 flows to compressor 93 and then to condenser 94 where it is condensed, utilizing water from the cooling water source (conventional apparatus for the vacuum condensation of low pressure steam produced by means of the heat of flue gases from cracking ovens or conventional absorption type of refrigeration apparatus utilizing ammonia or lithium salts and low pressure steam or hot water produced by means of the heat of flue gases from cracking ovens).
  • the as-produced ethane is drawn from the refrigeration cycle in the state of vapor and under a pressure of 7.6 abs.atm., through the piping 81.
  • FIG. 4 As a possible further example of refrigeration below minus 88° C., the diagram of FIG. 4 is reported, which uses a turbo-expanding machine which, differently from the turbine of FIG. 1, works in the superheated-gas field.
  • the mixture of the distillate of the demethanizing unit 7 coming from the reflux storage tank 8 is pre-cooled in the frigorie-recovery unit 101 and sent to the separator 102. From 102 the liquid, which is essentially methane and contains the last residues of ethylene and ethane, is sent back to the demethanizing unit 7 via the piping 103 and by means of the pump 104, thus recovering frigories in the exchanger 101.
  • the gas which is essentially hydrogen, is superheated in the frigorie-recovering unit 101 and then caused to expand in the first stage of the turbine 113.
  • the raw gas is introduced in the installation via the piping 1, is cooled to minus 59° C. with ethane in the refrigerating unit 2 and the condensed liquid is separated in the separator 3 and fed to the demethanizing unit 7 through the piping 4.
  • the residual gas in the separator 3 is cooled with ethane in the refrigerating unit 5.
  • the condensed liquid in its turn, is separated in the separator 201 and fed to the demethanizing unit 7 through the piping 202.
  • the demethanizing unit 7 is equipped with a condenser 204, the latter being cooled with boiling ethane under atmospherical pressure.
  • a fraction of the liquid condensed in the reflux storage tank 205 is sent back as a reflux stream to the demethanizing unit 7 through the pump 206.
  • the stream After vaporization in these two units, the stream is cooled in various frigorie-recovery units now shown in FIG. 5 for the sake of simplicity, and is recycled to the raw gas compressor.
  • the gas which has been separated in the reflux storage tank 205 is stripped of the residual ethylene and ethane in the packing 214 by the agency of the reflux as produced in the dephlegmator 215.
  • the distillate from the demethanizing unit which is the methane fraction, is heated, after having previously been expanded in the valve 203, in the frigorie recovery unit 210 and in various other frigorie recovery units not shown in FIG. 5, and delivered to the installation terminals via the piping 216.
  • the gas separated in the separator 201 and which contains hydrogen, methane, ethylene and ethane, is sent via the piping 220 to the frigorie recovery unit 210, thus producing a liquid fraction to be separated in the separator 230.
  • the latter liquid fraction which contains methane, and ethane, is sent back to the demethanizing unit 7 via the piping 232 by means of the pump 231 and after having been heated in the frigorie recovery unit 210.
  • the gas which composes the hydrogen fraction after having been heated in the frigorie recovery unit 210 and other units not shown in the drawings, is delivered via the piping 233 to the installation terminals.
  • FIG. 6 Another diagram for achieving the cooling to temperatures below minus 88° C., and which can be adopted when the raw gas contains significant amounts of methane (that is, when the raw materials sent to cracking are heavier than ethane, for example propane, naphtha or fuel-oil), is shown in FIG. 6.
  • This diagram exploits the turboexpansion of the methane fraction as produced at the head of the demethanizing unit.
  • the distillate of the demethanizing unit, emerging from the replux storage tank 8, is cooled in the frigorie recovery unit 301 and sent to the separator 305.
  • the liquid, which contains the ultimate fractions of ethylene and ethane, is sent back to the demethanizing unit 7 via the piping 306 by means of the pump 307, but after having previously been heated in the frigorie recovery unit 301.
  • the gas emerging from the separator 305, and which composes the methane fraction, is sent to the turbo-expansion unit 310 and subsequently heated in the frigorie recovery units 302 and 301 and in other like units not shown in the drawings and delivered to the installation terminals through the piping 314.
  • the residual gas in the separator 201 which contains hydrogen, methane, ethylene and ethane, is cooled in the frigorie recovery units 301 and 302 to be sent to the separator 320 wherein a liquid is separated which, via the piping 322, is sent back to the demethanizing unit 7.
  • the gas in the separator 320 which is the hydrogen fraction, is also heated in the frigorie recovering units 302 and 301 and in other like units not shown in the drawings and delivered at the installation terminals via the piping 323.
  • a portion of the as-produced hydrogen can be combined with the methane fraction through the piping 312 in order to increase the number of available frigories.
  • the installation is fed through the piping 1, with 32,169 kilograms an hour of a gas mixture under the pressure of 32.2 abs. atmospheres and at a temperature of 15° C., having the following composition:
  • the temperature of the mixture is brought to minus 34° C. and the separator 3 separates the liquid phase from the gaseous one.
  • the gaseous phase emerging from the head of the separator 3 under the pressure of 32.0 abs. atmospheres, has the following composition:
  • the liquid emerging from the bottom of the separator 3 has the following composition:
  • This liquid is fed to the demethanizing unit 7 via the piping 4.
  • the head stream of the demethanizing unit 7, said unit working with 60 plates and with a reflux ratio of 0.6 is condensed in the condenser 9 with refrigerating ethane down to a temperature of minus 82° C.
  • Such a stream is cooled in the frigorie recovering unit 11 and then partially liquefied and sent, via the piping 10, to the separator 12.
  • the gas is sent to the first stage, 14, of the turbine to be expanded therein, thwereas the liquid is caused to expand in the valve 16. Both the gas and the liquid, after the respective expansions, are sent to the separator 17.
  • the gas stream emerging from the separator 27, after that frigories have been recovered, is delivered to the installation terminals, whereas the liquid stream is pumped back to the demethanizing unit 7.
  • the bottom liquid stream of the demethanizing unit 7, having a temperature of minus 1° C. and a pressure of 31.5 abs. atmospheres has the following composition:
  • This liquid is sent to the deethanizing unit 33 which works with 40 plates and with a reflux ratio equal to 0.3, after having been expanded up to a pressure of 29 abs. atmospheres.
  • the distillate from the deethanizing unit 33 has at a temperature of minus 7° C. and under a pressure of 28.5 abs.atm. the following composition:
  • the bottom product is a liquid at the pressure of 17.8 abs.atm. and a temperature of minus 13.9° C. and has the following composition:
  • the liquid is sent to the refrigerating circuit.

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IT21580A/76 1976-03-26
IT21580/76A IT1058546B (it) 1976-03-26 1976-03-26 Processo per il frazoonamento mediante refrigerazione dei gas di cracking negli impianti per la produzione di etilene

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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4486209A (en) * 1981-07-07 1984-12-04 Snamprogetti, S.P.A. Recovering condensables from a hydrocarbon gaseous stream
US4695303A (en) * 1986-07-08 1987-09-22 Mcdermott International, Inc. Method for recovery of natural gas liquids
US4720293A (en) * 1987-04-28 1988-01-19 Air Products And Chemicals, Inc. Process for the recovery and purification of ethylene
US5253479A (en) * 1990-07-06 1993-10-19 Tpl S.P.A. Method and apparatus for recovery of ethylene and propylene from gas produced by the pyrolysis of hydrocarbons
US5361589A (en) * 1994-02-04 1994-11-08 Air Products And Chemicals, Inc. Precooling for ethylene recovery in dual demethanizer fractionation systems
US5377490A (en) * 1994-02-04 1995-01-03 Air Products And Chemicals, Inc. Open loop mixed refrigerant cycle for ethylene recovery
US5379597A (en) * 1994-02-04 1995-01-10 Air Products And Chemicals, Inc. Mixed refrigerant cycle for ethylene recovery
EP0675190A2 (en) * 1994-04-01 1995-10-04 The M.W. Kellogg Company Olefin recovery method
WO1996030708A1 (fr) * 1993-10-07 1996-10-03 David Pavlovich Sinelnikov Procede de traitement d'un pyrogaz avant separation du gaz, procede d'obtention de basses temperatures industrielles dans une machine de refrigeration par compression de vapeur par traitement du pyrogaz avant la separation du gaz
US20080209942A1 (en) * 2005-09-29 2008-09-04 China Petroleum & Chemical Corporation Process for recovering lower carbon olefins from product gas for production of olefins
WO2009083227A2 (de) * 2007-12-28 2009-07-09 Uhde Gmbh Verfahren und vorrichtung zur abtrennung von leicht siedenden komponenten aus kohlenwasserstoffgemischen
FR2939693A1 (fr) * 2008-12-16 2010-06-18 Inst Francais Du Petrole Nouveau procede de recuperation du co2 issu des fumees de regeneration d'une unite de craquage catalytique
US20110277500A1 (en) * 2010-05-12 2011-11-17 Linde Aktiengesellschaft Nitrogen removal from natural gas
EP3389807A4 (en) * 2015-12-18 2019-08-14 Bechtel Hydrocarbon Technology Solutions, Inc. SYSTEMS AND METHODS FOR RECOVERING LIGHT HYDROCARBONS DESIRED FROM REFINERY GASEOUS WASTE USING DOWNSTREAM TURBODETENDER
IT202200007049A1 (it) * 2022-04-08 2023-10-08 Alessandro Bugli Impianto e processo per la separazione di idrogeno da gas naturale
CN117029378A (zh) * 2023-07-27 2023-11-10 成都赛普瑞兴科技有限公司 原料气参与制冷的级联式制冷循环lng液化系统和方法
EP4345406A1 (en) * 2022-09-29 2024-04-03 Sulzer Management AG Plant and method for separating liquified petroleum gas from fuel gas by cryogenic distillation

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US4143521A (en) * 1977-02-08 1979-03-13 Stone & Webster Engineering Corporation Process for the production of ethylene
GB2146751B (en) * 1983-09-20 1987-04-23 Petrocarbon Dev Ltd Separation of hydrocarbon mixtures
AU572890B2 (en) * 1983-09-20 1988-05-19 Costain Petrocarbon Ltd. Separation of hydrocarbon mixtures

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US2775103A (en) * 1954-12-23 1956-12-25 Phillips Petroleum Co Hydrocarbon separation
US2823523A (en) * 1956-03-26 1958-02-18 Inst Gas Technology Separation of nitrogen from methane
US2960838A (en) * 1956-06-19 1960-11-22 Atomic Energy Authority Uk Hydrogen distillation plant
US2909905A (en) * 1957-06-05 1959-10-27 Black Sivalls & Bryson Inc Method for processing a natural gas stream
US3073129A (en) * 1958-11-28 1963-01-15 Air Liquide Process for degassing an ethylenic liquid
US3367122A (en) * 1964-03-12 1968-02-06 Conch Int Methane Ltd Regasifying liquefied natural gas by heat exchange with fractionator overhead streams
US3433026A (en) * 1966-11-07 1969-03-18 Judson S Swearingen Staged isenthalpic-isentropic expansion of gas from a pressurized liquefied state to a terminal storage state
US3756036A (en) * 1971-04-20 1973-09-04 Phillips Petroleum Co Demethanizing method and apparatus
US3938934A (en) * 1974-11-08 1976-02-17 Scm Corporation Fuel economizer process and apparatus

Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4486209A (en) * 1981-07-07 1984-12-04 Snamprogetti, S.P.A. Recovering condensables from a hydrocarbon gaseous stream
US4695303A (en) * 1986-07-08 1987-09-22 Mcdermott International, Inc. Method for recovery of natural gas liquids
US4720293A (en) * 1987-04-28 1988-01-19 Air Products And Chemicals, Inc. Process for the recovery and purification of ethylene
US5253479A (en) * 1990-07-06 1993-10-19 Tpl S.P.A. Method and apparatus for recovery of ethylene and propylene from gas produced by the pyrolysis of hydrocarbons
US5946941A (en) * 1993-10-07 1999-09-07 Sinelnikov; David Pavlovich Method for processing pyrolysis gas prior to gas separation and method for producing low temperature cold in a vapor compression refrigerating machine during processing of pyrolysis gas prior to gas separation
WO1996030708A1 (fr) * 1993-10-07 1996-10-03 David Pavlovich Sinelnikov Procede de traitement d'un pyrogaz avant separation du gaz, procede d'obtention de basses temperatures industrielles dans une machine de refrigeration par compression de vapeur par traitement du pyrogaz avant la separation du gaz
US5379597A (en) * 1994-02-04 1995-01-10 Air Products And Chemicals, Inc. Mixed refrigerant cycle for ethylene recovery
US5497626A (en) * 1994-02-04 1996-03-12 Air Products And Chemicals, Inc. Open loop mixed refrigerant cycle for ethylene recovery
US5502972A (en) * 1994-02-04 1996-04-02 Air Products And Chemicals, Inc. Mixed refrigerant cycle for ethylene recovery
US5377490A (en) * 1994-02-04 1995-01-03 Air Products And Chemicals, Inc. Open loop mixed refrigerant cycle for ethylene recovery
US5361589A (en) * 1994-02-04 1994-11-08 Air Products And Chemicals, Inc. Precooling for ethylene recovery in dual demethanizer fractionation systems
SG81846A1 (en) * 1994-02-04 2001-07-24 Air Prod & Chem Precooling for ethylene recovery in dual demethanizer fractionation systems
EP0675190A2 (en) * 1994-04-01 1995-10-04 The M.W. Kellogg Company Olefin recovery method
EP0675190A3 (en) * 1994-04-01 2007-08-08 The M.W. Kellogg Company Olefin recovery method
US20080209942A1 (en) * 2005-09-29 2008-09-04 China Petroleum & Chemical Corporation Process for recovering lower carbon olefins from product gas for production of olefins
US7707852B2 (en) * 2005-09-29 2010-05-04 China Petroleum & Chemical Corporation Process for recovering lower carbon olefins from product gas for production of olefins
WO2009083227A3 (de) * 2007-12-28 2009-09-17 Uhde Gmbh Verfahren und vorrichtung zur abtrennung von leicht siedenden komponenten aus kohlenwasserstoffgemischen
US20110041550A1 (en) * 2007-12-28 2011-02-24 Uhde Gmbh Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures
WO2009083227A2 (de) * 2007-12-28 2009-07-09 Uhde Gmbh Verfahren und vorrichtung zur abtrennung von leicht siedenden komponenten aus kohlenwasserstoffgemischen
US8784760B2 (en) 2008-12-16 2014-07-22 IFP Energies Nouvelles Process for recovering CO2 from regeneration flue gas coming from a catalytic cracking unit
FR2939693A1 (fr) * 2008-12-16 2010-06-18 Inst Francais Du Petrole Nouveau procede de recuperation du co2 issu des fumees de regeneration d'une unite de craquage catalytique
WO2010070212A1 (fr) * 2008-12-16 2010-06-24 Ifp Nouveau procede de recuperation du co2 issu des fumees de regeneration d'une unite de craquage catalytique
US20110277500A1 (en) * 2010-05-12 2011-11-17 Linde Aktiengesellschaft Nitrogen removal from natural gas
US9003829B2 (en) * 2010-05-12 2015-04-14 Linde Aktiengesellschaft Nitrogen removal from natural gas
EP3389807A4 (en) * 2015-12-18 2019-08-14 Bechtel Hydrocarbon Technology Solutions, Inc. SYSTEMS AND METHODS FOR RECOVERING LIGHT HYDROCARBONS DESIRED FROM REFINERY GASEOUS WASTE USING DOWNSTREAM TURBODETENDER
IT202200007049A1 (it) * 2022-04-08 2023-10-08 Alessandro Bugli Impianto e processo per la separazione di idrogeno da gas naturale
WO2023194967A1 (en) * 2022-04-08 2023-10-12 Alessandro Bugli Plant and process for separating hydrogen from natural gas
EP4345406A1 (en) * 2022-09-29 2024-04-03 Sulzer Management AG Plant and method for separating liquified petroleum gas from fuel gas by cryogenic distillation
WO2024068241A1 (en) * 2022-09-29 2024-04-04 Sulzer Management Ag Plant and method for separating liquified petroleum gas from fuel gas by cryogenic distillation
CN117029378A (zh) * 2023-07-27 2023-11-10 成都赛普瑞兴科技有限公司 原料气参与制冷的级联式制冷循环lng液化系统和方法

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FR2345412A1 (fr) 1977-10-21
DE2713359B2 (de) 1979-05-17
FI770813A (no) 1977-09-27
FR2345412B1 (no) 1980-02-29
IE45273B1 (en) 1982-07-28
BE852922A (fr) 1977-09-26
NO150079B (no) 1984-05-07
IT1058546B (it) 1982-05-10
SE420915B (sv) 1981-11-09
AR212989A1 (es) 1978-11-30
GB1571073A (en) 1980-07-09
NL173844C (nl) 1984-03-16
SE7703479L (sv) 1977-09-27
IS1055B6 (is) 1981-08-25
CA1047386A (en) 1979-01-30
DK134077A (da) 1977-09-27
DE2713359A1 (de) 1977-09-29
NL173844B (nl) 1983-10-17
IE45273L (en) 1977-09-26
IS2381A7 (is) 1977-09-27
NO150079C (no) 1984-08-22
NL7703283A (nl) 1977-09-28
NO771073L (no) 1977-09-27

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